CN108046293A - Recycle the method that heat alkali liquid is used for salt manufacturing bittern purification - Google Patents

Recycle the method that heat alkali liquid is used for salt manufacturing bittern purification Download PDF

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Publication number
CN108046293A
CN108046293A CN201711217270.8A CN201711217270A CN108046293A CN 108046293 A CN108046293 A CN 108046293A CN 201711217270 A CN201711217270 A CN 201711217270A CN 108046293 A CN108046293 A CN 108046293A
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China
Prior art keywords
level
alkali liquid
heat alkali
slurries
mud
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Pending
Application number
CN201711217270.8A
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Chinese (zh)
Inventor
李元海
彭善俊
黄登兵
张立武
王洪林
李亮
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Hubei Shuanghuan Science and Technology Stock Co Ltd
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Hubei Shuanghuan Science and Technology Stock Co Ltd
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Priority to CN201711217270.8A priority Critical patent/CN108046293A/en
Publication of CN108046293A publication Critical patent/CN108046293A/en
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    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01D—COMPOUNDS OF ALKALI METALS, i.e. LITHIUM, SODIUM, POTASSIUM, RUBIDIUM, CAESIUM, OR FRANCIUM
    • C01D3/00—Halides of sodium, potassium or alkali metals in general
    • C01D3/04—Chlorides
    • C01D3/06—Preparation by working up brines; seawater or spent lyes
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01D—COMPOUNDS OF ALKALI METALS, i.e. LITHIUM, SODIUM, POTASSIUM, RUBIDIUM, CAESIUM, OR FRANCIUM
    • C01D3/00—Halides of sodium, potassium or alkali metals in general
    • C01D3/14—Purification
    • C01D3/16—Purification by precipitation or adsorption
    • C—CHEMISTRY; METALLURGY
    • C05—FERTILISERS; MANUFACTURE THEREOF
    • C05D—INORGANIC FERTILISERS NOT COVERED BY SUBCLASSES C05B, C05C; FERTILISERS PRODUCING CARBON DIOXIDE
    • C05D3/00—Calcareous fertilisers
    • C05D3/02—Calcareous fertilisers from limestone, calcium carbonate, calcium hydrate, slaked lime, calcium oxide, waste calcium products

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  • Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Inorganic Chemistry (AREA)
  • Engineering & Computer Science (AREA)
  • Materials Engineering (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Fertilizers (AREA)
  • Separation Of Suspended Particles By Flocculating Agents (AREA)

Abstract

The present invention relates to bittern purifying fields, disclose a kind of method for recycling heat alkali liquid and being used for salt manufacturing bittern purification, comprise the following steps：Former halogen is introduced into first-stage reactor, soda bath is added in and is sufficiently stirred and reacted, obtain and complete level-one slurries；Level-one slurries are settled, obtain level-one supernatant liquor and level-one lower floor mud；Level-one supernatant liquor is introduced into second reactor, while the heat alkali liquid discharged by heat alkali liquid tower is introduced in second reactor, is sufficiently stirred and is reacted, obtain and complete two level slurries；Two level slurries are settled, obtain Lower TierII clear liquid and Upper Tier II mud；Lower TierII clear liquid is introduced into salt making apparatus, is evaporated crystallization production product salt.The method that present invention recycling heat alkali liquid is used for salt manufacturing bittern purification reduces the use of solid soda ash while solving heat alkali liquid Utilizing question, considerably reduces the production cost of enterprise, and it is high to purify removal efficiency.

Description

Recycle the method that heat alkali liquid is used for salt manufacturing bittern purification
Technical field
The present invention relates to bittern purifying field, more particularly to a kind of method for recycling heat alkali liquid and being used for salt manufacturing bittern purification.
Background technology
Weight alkali calcining decomposes the gas generated, contains a certain amount of thin ground caustic, after clear water spray washing, thin ground caustic dissolving In clear water, formed and contain certain Na2CO3Solution, be commonly called as heat alkali liquid.Heat alkali liquid constantly dissolves alkali in washing process is cycled Dirt is constantly raised containing alkali concn, and the ability of dissolving alkali dirt constantly declines, and washing effect is deteriorated, it is therefore desirable to stove be continuously replenished The lime set that is gas-cooled (or clear water), and exclusive segment heat alkali liquid is to keep the dynamic equilibrium of thermokalite liquid measure.
In the prior art, joining alkali-ammonia alkali Joint Production enterprise, row pollutes heat alkali liquid outside in order to prevent, can only generally send Toward ammonia alkali device, though having prevented pollution, the sodium carbonate and sodium acid carbonate in heat alkali liquid react in ammonia still with ammonium chloride gives birth to It into sodium chloride, is discharged with waste ammonia-soda solution, results in the loss of soda ash.
The purification of salt manufacturing bittern in soda ash enterprise is general to use " caustic soda-soda ash " method (NaOH-Na2CO3), that is, pass through outsourcing Or self-produced caustic soda, using self-produced soda ash, remove Ca2+、Mg2+, realize bittern purifying.This purification method needs to consume soda ash, makes Into lost revenue.
The content of the invention
The purpose of the present invention provides a kind of recycling heat alkali liquid and is purified for salt manufacturing bittern aiming at the deficiency of above-mentioned technology Method, while solving heat alkali liquid Utilizing question, reduce the use of solid soda ash, considerably reduce the life of enterprise Cost is produced, and it is high to purify removal efficiency.
To achieve the above object, a kind of method for recycling heat alkali liquid and being used for salt manufacturing bittern purification of the present invention, including following step Suddenly：
A former halogen) is introduced into first-stage reactor, soda bath is added in and is sufficiently stirred and reacted, the reaction time is 30~100 Minute, it obtains and completes level-one slurries；
B) by the step A) in obtain level-one slurries settle, the sedimentation time be 60~150 minutes, obtain level-one Supernatant liquor and level-one lower floor mud；
C) by the step B) in obtain level-one supernatant liquor introduce second reactor, level-one lower floor mud is drained into mud Collection device is starched, while the heat alkali liquid discharged by heat alkali liquid tower is introduced in second reactor, by level-one supernatant liquor and thermokalite Liquid, which is sufficiently stirred, to be reacted, and the reaction time is 30~100 minutes, obtains and completes two level slurries；
D) by the step C) in obtain two level slurries settle, the sedimentation time be 60~150 minutes, obtain two level Supernatant liquor and Upper Tier II mud；
E) by the step D) in obtain Lower TierII clear liquid introduce salt making apparatus, be evaporated crystallization production salt production Product, and obtained salt-making mother liquor is introduced into the step A) first-stage reactor in, reaction is participated in again, by Upper Tier II mud Drain into slurry collecting device.
Further, the step C is made by heating unit) in the heat alkali liquid temperature that introduces for 70~80 DEG C, prevent temperature Spending low causes Na2CO3It is precipitated.
Further, the step A) in the soda bath that adds in NaOH content for 10~19mol/L, soda bath With the volume ratio 1~3 of former halogen:100.
Further, make the step C by adjusting device) in Na in the heat alkali liquid that is introduced into2CO3Content for 1~ 2.5mol/L, the volume ratio 1~3 of heat alkali liquid and level-one supernatant liquor:100.
Further, the step B) by the step A) in the level-one slurries that obtain add flocculant when being settled, Additive amount is 1~5ppm, the step D) by the step C) in the two level slurries that obtain add flocculant when being settled, add Dosage is 1~5ppm.
Further, level-one lower floor mud and Upper Tier II mud that slurry collecting device is collected through thickening are filtered, washed Wash, be dehydrated and drying process after become chemical fertilizer, improve income, reduce cost.
Reaction mechanism in the present invention using soda bath and heat alkali liquid is as follows：
Utilize " the OH in NaOH-" removal Mg2+, utilize heat alkali liquid (main component Na2CO3) in " CO3 2-" removal Ca2+, Its key reaction formula is：
2NaOH+MgSO4=Mg (OH)2↓+Na2SO4
Na2CO3+CaSO4=CaCO3↓+Na2SO4
By by Mg (OH)2And CaCO3Precipitation, so as to remove the Mg in former halogen2+And Ca2+。
Compared with prior art, the present invention it has the following advantages：
1st, extra heat alkali liquid is solved heat alkali liquid Utilizing question, reduces environmental pollution for brine refining；
2nd, by using heat alkali liquid, reduce solid soda ash use, reduce production cost；
3rd, matched by adjusting soda bath, heat alkali liquid, reaction time and sedimentation time, improve purification removal efficiency.
Specific embodiment
With reference to embodiment, the present invention is described in further detail, convenient for more clearly understanding the present invention, but it Not to the present invention form limit.
Embodiment 1
Preparation process：
A former halogen) is introduced into first-stage reactor, soda bath is added in and is sufficiently stirred and reacted, NaOH in soda bath Content is the volume ratio 1 of 10mol/L, soda bath and former halogen:100, the reaction time is 30 minutes, obtains and completes level-one slurries；
B) by step A) in the level-one slurries that obtain settle, add flocculant, additive amount 1ppm, the sedimentation time is 60 minutes, obtain level-one supernatant liquor and level-one lower floor mud；
C) by step B) in obtain level-one supernatant liquor introduce second reactor, by level-one lower floor mud drain into mud receive Acquisition means, while the heat alkali liquid discharged by heat alkali liquid tower is introduced in second reactor, the heat alkali liquid temperature of introducing is 70 DEG C, heat Na in lye2CO3Content for 10mol/L, the volume ratio 1 of heat alkali liquid and level-one supernatant liquor:100, by level-one supernatant liquor and Heat alkali liquid, which is sufficiently stirred, to be reacted, and the reaction time is 30 minutes, obtains and completes two level slurries；
D) by step C) in the two level slurries that obtain settle, add flocculant, additive amount 1ppm, the sedimentation time is 60 minutes, obtain Lower TierII clear liquid and Upper Tier II mud；
E) by step D) in obtain Lower TierII clear liquid introduce salt making apparatus, be evaporated crystallization production product salt, and Obtained salt-making mother liquor is introduced into step A) first-stage reactor in, again participate in reaction, Upper Tier II mud is drained into mud Collection device, the level-one lower floor mud and Upper Tier II mud that slurry collecting device is collected through thickening filtering, washing, dehydration and Become chemical fertilizer after drying process.
Embodiment 2
Preparation process：
A former halogen) is introduced into first-stage reactor, soda bath is added in and is sufficiently stirred and reacted, NaOH in soda bath Content is the volume ratio 3 of 19mol/L, soda bath and former halogen:100, the reaction time is 100 minutes, obtains and completes level-one slurries；
B) by step A) in the level-one slurries that obtain settle, add flocculant, additive amount 5ppm, the sedimentation time is 150 minutes, obtain level-one supernatant liquor and level-one lower floor mud；
C) by step B) in obtain level-one supernatant liquor introduce second reactor, by level-one lower floor mud drain into mud receive Acquisition means, while the heat alkali liquid discharged by heat alkali liquid tower is introduced in second reactor, the heat alkali liquid temperature of introducing is 80 DEG C, heat Na in lye2CO3Content for 2.5mol/L, the volume ratio 3 of heat alkali liquid and level-one supernatant liquor:100, by level-one supernatant liquor It is sufficiently stirred and is reacted with heat alkali liquid, the reaction time is 100 minutes, obtains and completes two level slurries；
D) by step C) in the two level slurries that obtain settle, add flocculant, additive amount 5ppm, the sedimentation time is 150 minutes, obtain Lower TierII clear liquid and Upper Tier II mud；
E) by step D) in obtain Lower TierII clear liquid introduce salt making apparatus, be evaporated crystallization production product salt, and Obtained salt-making mother liquor is introduced into step A) first-stage reactor in, again participate in reaction, Upper Tier II mud is drained into mud Collection device, the level-one lower floor mud and Upper Tier II mud that slurry collecting device is collected through thickening filtering, washing, dehydration and Become chemical fertilizer after drying process.
Embodiment 3
Preparation process：
A former halogen) is introduced into first-stage reactor, soda bath is added in and is sufficiently stirred and reacted, NaOH in soda bath Content is the volume ratio 2 of 15mol/L, soda bath and former halogen:100, the reaction time is 60 minutes, obtains and completes level-one slurries；
B) by step A) in the level-one slurries that obtain settle, add flocculant, additive amount 2ppm, the sedimentation time is 100 minutes, obtain level-one supernatant liquor and level-one lower floor mud；
C) by step B) in obtain level-one supernatant liquor introduce second reactor, by level-one lower floor mud drain into mud receive Acquisition means, while the heat alkali liquid discharged by heat alkali liquid tower is introduced in second reactor, the heat alkali liquid temperature of introducing is 75 DEG C, heat Na in lye2CO3Content for 1.5mol/L, the volume ratio 1.5 of heat alkali liquid and level-one supernatant liquor:100, level-one upper strata is clear Liquid and heat alkali liquid, which are sufficiently stirred, to be reacted, and the reaction time is 60 minutes, obtains and completes two level slurries；
D) by step C) in the two level slurries that obtain settle, add flocculant, additive amount 2ppm, the sedimentation time is 100 minutes, obtain Lower TierII clear liquid and Upper Tier II mud；
E) by step D) in obtain Lower TierII clear liquid introduce salt making apparatus, be evaporated crystallization production product salt, and Obtained salt-making mother liquor is introduced into step A) first-stage reactor in, again participate in reaction, Upper Tier II mud is drained into mud Collection device, the level-one lower floor mud and Upper Tier II mud that slurry collecting device is collected through thickening filtering, washing, dehydration and Become chemical fertilizer after drying process.
Embodiment 4
Preparation process：
A former halogen) is introduced into first-stage reactor, soda bath is added in and is sufficiently stirred and reacted, NaOH in soda bath Content is the volume ratio 2.5 of 17mol/L, soda bath and former halogen:100, the reaction time is 80 minutes, obtains and completes level-one slurry Liquid；
B) by step A) in the level-one slurries that obtain settle, add flocculant, additive amount 4ppm, the sedimentation time is 120 minutes, obtain level-one supernatant liquor and level-one lower floor mud；
C) by step B) in obtain level-one supernatant liquor introduce second reactor, by level-one lower floor mud drain into mud receive Acquisition means, while the heat alkali liquid discharged by heat alkali liquid tower is introduced in second reactor, the heat alkali liquid temperature of introducing is 78 DEG C, heat Na in lye2CO3Content for 2mol/L, the volume ratio 2 of heat alkali liquid and level-one supernatant liquor:100, by level-one supernatant liquor and Heat alkali liquid, which is sufficiently stirred, to be reacted, and the reaction time is 80 minutes, obtains and completes two level slurries；
D) by step C) in the two level slurries that obtain settle, add flocculant, additive amount 3ppm, the sedimentation time is 120 minutes, obtain Lower TierII clear liquid and Upper Tier II mud；
E) by step D) in obtain Lower TierII clear liquid introduce salt making apparatus, be evaporated crystallization production product salt, and Obtained salt-making mother liquor is introduced into step A) first-stage reactor in, again participate in reaction, Upper Tier II mud is drained into mud Collection device, the level-one lower floor mud and Upper Tier II mud that slurry collecting device is collected through thickening filtering, washing, dehydration and Become chemical fertilizer after drying process.
1 calcium ion of table and magnesium ion removal efficiency
According to table 1 as a result, by adjusting soda bath, heat alkali liquid, reaction time and sedimentation time match, obtained compared with High purification removal efficiency.
The method that present invention recycling heat alkali liquid is used for salt manufacturing bittern purification subtracts while solving heat alkali liquid Utilizing question Lack the use of solid soda ash, considerably reduce the production cost of enterprise, and it is high to purify removal efficiency.

Claims (6)

  1. A kind of 1. method for recycling heat alkali liquid and being used for salt manufacturing bittern purification, it is characterised in that：Comprise the following steps：
    A former halogen) is introduced into first-stage reactor, soda bath is added in and is sufficiently stirred and reacted, the reaction time is 30~100 points Clock obtains and completes level-one slurries；
    B) by the step A) in the level-one slurries that obtain settle, the sedimentation time is 60~150 minutes, obtains level-one upper strata Clear liquid and level-one lower floor mud；
    C) by the step B) in obtain level-one supernatant liquor introduce second reactor, by level-one lower floor mud drain into mud receive Acquisition means, while the heat alkali liquid discharged by heat alkali liquid tower is introduced in second reactor, level-one supernatant liquor and heat alkali liquid are filled Stirring is divided to be reacted, the reaction time is 30~100 minutes, obtains and completes two level slurries；
    D) by the step C) in obtain two level slurries settle, the sedimentation time be 60~150 minutes, obtain Lower TierII Clear liquid and Upper Tier II mud；
    E) by the step D) in obtain Lower TierII clear liquid introduce salt making apparatus, be evaporated crystallization production product salt, and Obtained salt-making mother liquor is introduced into the step A) first-stage reactor in, again participate in reaction, Upper Tier II mud is drained into Slurry collecting device.
  2. 2. the method that heat alkali liquid is used for salt manufacturing bittern purification is recycled according to claim 1, it is characterised in that：It is filled by heating Putting makes the step C) in introduce heat alkali liquid temperature be 70 DEG C~80 DEG C.
  3. 3. the method that heat alkali liquid is used for salt manufacturing bittern purification is recycled according to claim 1, it is characterised in that：The step A) The content of NaOH is the volume ratio 1~3 of 10~19mol/L, soda bath and former halogen in the soda bath of middle addition:100.
  4. 4. the method that heat alkali liquid is used for salt manufacturing bittern purification is recycled according to claim 1, it is characterised in that：By adjusting dress Putting makes the step C) in Na in the heat alkali liquid that is introduced into2CO3Content for 1~2.5mol/L, heat alkali liquid and level-one supernatant liquor Volume ratio 1~3:100.
  5. 5. the method that heat alkali liquid is used for salt manufacturing bittern purification is recycled according to claim 1, it is characterised in that：The step B) By the step A) in the level-one slurries that obtain flocculant is added when being settled, additive amount is 1~5ppm, the step D) will The step C) in the two level slurries that obtain flocculant is added when being settled, additive amount is 1~5ppm.
  6. 6. the method that heat alkali liquid is used for salt manufacturing bittern purification is recycled according to claim 1, it is characterised in that：By slurry collecting The level-one lower floor mud and Upper Tier II mud that device is collected become chemical fertilizer after thickening filtering, washing, dehydration and drying process.
CN201711217270.8A 2017-11-28 2017-11-28 Recycle the method that heat alkali liquid is used for salt manufacturing bittern purification Pending CN108046293A (en)

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Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN113173589A (en) * 2020-11-11 2021-07-27 内蒙古兰太钠业有限责任公司 Preparation system and process method of liquid salt for alkali production

Citations (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN1107121A (en) * 1993-12-08 1995-08-23 山东潍坊纯碱厂 Method of preparing refined brine by using bittern
CN101691239A (en) * 2009-09-30 2010-04-07 达州市恒成能源（集团）有限责任公司 Comprehensive utilization method for bittern
CN102009987A (en) * 2010-12-02 2011-04-13 河南神马氯碱化工股份有限公司 Brine refining process for removing calcium and magnesium by one step
CN103880042A (en) * 2014-04-14 2014-06-25 唐山三友化工股份有限公司 Brine refinement technique
CN106745115A (en) * 2017-01-19 2017-05-31 中国中轻国际工程有限公司 Calcium and magnesium mud production magnesium sulfate and the calcium carbonate technique of a kind of utilization bittern purifying

Patent Citations (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN1107121A (en) * 1993-12-08 1995-08-23 山东潍坊纯碱厂 Method of preparing refined brine by using bittern
CN101691239A (en) * 2009-09-30 2010-04-07 达州市恒成能源（集团）有限责任公司 Comprehensive utilization method for bittern
CN102009987A (en) * 2010-12-02 2011-04-13 河南神马氯碱化工股份有限公司 Brine refining process for removing calcium and magnesium by one step
CN103880042A (en) * 2014-04-14 2014-06-25 唐山三友化工股份有限公司 Brine refinement technique
CN106745115A (en) * 2017-01-19 2017-05-31 中国中轻国际工程有限公司 Calcium and magnesium mud production magnesium sulfate and the calcium carbonate technique of a kind of utilization bittern purifying

Non-Patent Citations (1)

* Cited by examiner, † Cited by third party
Title
王刚等编: "《盐化工工艺学》", 31 December 2016, 清华大学出版社 *

Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN113173589A (en) * 2020-11-11 2021-07-27 内蒙古兰太钠业有限责任公司 Preparation system and process method of liquid salt for alkali production

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Application publication date: 20180518